Methods of producing calcined coke from bio-oil and calcined coke produced thereby

ABSTRACT

Disclosed are methods of producing calcined coke from bio-oil from a biomass feedstock. Also disclosed are calcined cokes produced by such methods.

REFERENCE TO RELATED APPLICATION

This application claims the benefit of U.S. Provisional Application No.62/094,618, filed 19 Dec. 2014, which is incorporated herein byreference in its entirety.

BACKGROUND OF THE INVENTION

Disclosed are methods of producing calcined coke from bio-oil from abiomass feedstock, involving (1) subjecting the bio-oil to atmosphericdistillation in a batch or continuous distillation unit and/orsubsequently to vacuum distillation in a batch or continuous vacuumdistillation unit to produce coke (i.e. distillation bottoms), (2)subjecting the coke bottoms to (a) stepwise calcination at about 400° toabout 1000° C. for about 1 to about 30 minutes in an inert gasatmosphere in a reactor to produce devolatilized coke, optionallycooling the devolatilized coke, removing the devolatilized coke from thereactor and optionally crushing the devolatilized coke, and stepwisecalcining the devolatilized coke at about 1200° C. to about 1400° C. forup to about 2 hours in an inert gas atmosphere in a reactor to producecalcined coke; or (b) devolatilization at about 400° to about 1000° C.for about 1 to about 30 minutes in an inert gas atmosphere in a reactorto produce devolatilized coke and stepwise calcining the devolatilizedcoke at about 1200° C. to about 1400° C. for up to about 2 hours in aninert gas atmosphere in the same reactor to produce calcined coke; or(c) stepwise heating at about 250° to about 400° C. for about 2 to about10 hours, then subsequent stepwise calcination at about 400° to about1000° C. for about 0.5 to about 5 hr to produce devolatilized coke, thencalcining said devolatilized coke at about 1200° C. to about 1400° C.for about 1 to about 4 hours in an inert gas atmosphere in a batch orcontinuous reactor to produce calcined coke; or (d) stepwise calcinationin a continuous calcining reactor between about 200° to about 1400° C.with up to about 1 hr residence time. Also disclosed are calcined cokesproduced by such methods.

Since the worldwide consumption of liquid transportation fuels isoutpacing the finite supply of fossil fuels, research for petroleumreplacements have focused squarely on fuels (Mangla, V. et al., Curr.Chem. Biol., 7: 96-103 (2013); Sorrell, S., et al., Energy Policy, 38:5290-5295 (2010)). Although finished motor fuels comprise the bulk ofpetrochemical refinery outputs, the world economy relies heavily on manyeveryday products that emanate from petroleum (U.S. EnvironmentalProtection Agency,http://www.eia.gov/dnav/pet/pet_cons_psup_dc_nus_mbbl_a.htm). Some basicexamples include commodity chemicals like BTEX petrochemical feedstock(benzene-toluene-ethylbenzene-xylenes), phenolic resins for plastics,waxes and lubricants, and asphalt for roofing and road pavement.Altogether, non-fuels co-products comprise 15-20% of all petroleumproducts (U.S. Environmental Protection Agency,http://www.eia.gov/dnav/pet/pet_cons_psup_dc_nus_mbbl_a.htm).Furthermore, many petrochemical refineries rely on non-fuelsapplications for the large majority of their product sales. Therefore, astrategy for renewable fuels must be coupled with a strategy to bringeconomic value via petrochemical co-product replacements. As an example,production of biodiesel was found to be economically viable due to thefeasibility of producing glycerol in parallel (Haas, M. J., et al.,Bioresource Technol., 97: 671-678 (2006); Lopes, D. C., et al., Energ.Econ., 40: 819-824 (2013)).

One of the most crucial yet least discussed co-products of value ispetroleum coke (termed “petcoke”). Typically, the residuals remainingafter vacuum distillation of crude oil (>600° C.) enter a delayed cokerunit which thermally cracks the residual into petcoke and lighter fuelcomponents (Olsen, T., “Chemical and Engineering Practice,” An OilRefinery Walk-Through, pp. 34-40, May 2014). Petcoke can be used as-isto substitute for coal in fuel applications or, if the metals and sulfurcontents are low enough, can be calcined into coke products suitable foruse in aluminum smelting anodes. The latter application alone can absorbmore than 70% of the petcoke market (Zhang, Z., and T. Wang, J. Therm.Sci. Eng. App., 2: 021006-1-021006-8 (2010); Ellis, P. J., and C. A.Paul, “Tutorial: Petroleum Coke Calcining and Uses of Calcined PetroleumCoke,” IN AIChE 2000 Spring National Meeting,Third InternationalConference on Refining Processes, Session T9005, Atlanta, Ga., 2000).Other high-volume markets for calcined coke utilize the remaining 30%for production of graphite, steel, and titanium dioxide (Ellis and Paul2000; Paul, C. A., and L. E. Herrington, “Desulfurization of petroleumcoke beyond 1600° C.” IN Light Metals: Proceedings of Sessions, TMSAnnual Meeting, Warrendale, Pa., 597-601, 2001). Globally, 50 M metrictons/year of aluminum are produced from approximately 25M metric tons ofcarbon per year, and low-quality coke can cost smelters more than$100/metric ton of product in consumption costs (“The carbon anodemarket-a global viewpoint (Interview with Michael Wrotniak, CEO ofAminco Resources),” Aluminum, June 2014; Alcoa Inc., “Aluminum smeltingtechnical article,”http://www.alcoa.com/global/en/about_alcoa/pdf/Smeltingpaper.pdf).Petcoke demand continues to rise annually, for which the U.S. providesmore than half the global supply, and the market has gone wanting forsources that are renewable due to several sustainability factors (“Asiandemand spurs U.S. net exports of petroleum coke to higher levels inearly 2012,” Petroleum Supply Monthly, U.S. Energy InformationAdministration, 25 May 2012,http://www.eia.gov/todayinenergy/detail.cfm?id=6430#; Chmelar, J., Sizereduction and specification of granular petrol coke with respect tochemical and physical properties, Doctoral thesis, Norwegian Universityof Science and Technology, 2006). Although aluminum smelting cantolerate 2-3% sulfur, further reduction of sulfur is desired due to thecorrosive nature of sulfur during the smelting process, which reducesanode lifetime (Edwards, L., “Impurity level distribution in gpc and cpcand impact on anode properties,” IN Light Metals 2014: The Minerals,Metals, & Materials Society, Wiley, 2014, pp. 1093-1098). Even 1% sulfurruins steel mechanical properties through brittleness. Demand forhigh-quality calcined coke is hampered by the continually decliningquality of petcoke, via high sulfur and metals content (Ni, V)(Edwards,L. C., “Responding to Changes in Coke Quality,” IN Proceedings of the10th Australian Smelting Technology Conference, Terrigal, NSW, 2007;Edwards, L. C., et al., “A review of coke and anode desulfurization,” INLight Metals, Wiley, 2007). Calciners currently must desulfurize coke tomeet demand for both anodes and steel, which intensively increasesprocessing costs.

Extremely high temperatures and/or pressures are required to initiateand propagate coke polymerization. Hence, one cannot easily produce cokeas a side product from enzymatic processes for cellulosic ethanol orlipid-based biodiesel processes since they operate under mild conditions(i.e., low temperature and pressure). While coke does come about as aside product in hydrodeoxygenation, coke deactivates catalysts andblocks catalyst pores, which makes coking an unwanted phenomenon insitu. Incidentally, thermochemical methods of biofuels production (e.g.,gasification, pyrolysis) are well-suited for isolating biochar solidresidue in parallel to the liquid crude oil that is produced(“bio-oil”). However, the high metals content of biochar renders itunsuitable for refined coke and much more amenable for soil remediation(Gurtler, J., et al., Foodborne Pathog. Disease, 11: 215-223 (2014)).When bio-oil is distilled, the solid residue that remains leftover couldserve as a precursor for biorenewable calcined coke. Traditional bio-oildistillation had been largely ignored due to significant yield lossesfrom thermal instabilities. Recently, we demonstrated the high-yielddistillation of tail-gas reactive pyrolysis (TGRP) bio-oil under normalatmospheric distillation conditions (Elkasabi, Y., et al., ACSSustainable Chem. Eng., p. 10.1021/sc5002879 (2014)). The TGRP processdoes not utilize any catalyst nor external hydrogen, yet surprisinglyproduces bio-oils with <10 wt % oxygen, comparable to catalytic fastpyrolysis bio-oil (vs. 34-40 wt % in traditional bio-oil produced bytraditional fast pyrolysis), which gives rise to thermally stablebio-oils for distillation (Mullen, C. A., et al., Energy Fuels, 27:387-3874 (2013)). Solid residues remaining post-distillation amountto >15% of the starting bio-oil, which amounts to a significant profitif it can be processed into suitable petroleum coke.

Herein we discuss bio-oil distillate bottoms as a source for renewablecalcined coke in various applications.

SUMMARY OF THE INVENTION

Disclosed are methods of producing calcined coke from bio-oil from abiomass feedstock, involving (1) subjecting the bio-oil to atmosphericdistillation in a batch or continuous distillation unit and/orsubsequently to vacuum distillation in a batch or continuous vacuumdistillation unit to produce coke (i.e. distillation bottoms), (2)subjecting the coke bottoms to (a) stepwise calcination at about 400° toabout 1000° C. for about 1 to about 30 minutes in an inert gasatmosphere in a reactor to produce devolatilized coke, optionallycooling the devolatilized coke, removing the devolatilized coke from thereactor and optionally crushing the devolatilized coke, and stepwisecalcining the devolatilized coke at about 1200° C. to about 1400° C. forup to about 2 hours in an inert gas atmosphere in a reactor to producecalcined coke; or (b) devolatilization at about 400° to about 1000° C.for about 1 to about 30 minutes in an inert gas atmosphere in a reactorto produce devolatilized coke and stepwise calcining the devolatilizedcoke at about 1200° C. to about 1400° C. for up to about 2 hours in aninert gas atmosphere in the same reactor to produce calcined coke; or(c) stepwise heating at about 250° to about 400° C. for about 2 to about10 hours, then subsequent stepwise calcination at about 400 to about1000° C. for about 0.5 to about 5 hr to produce devolatilized coke, thencalcining said devolatilized coke at about 1200° C. to about 1400° C.for about 1 to about 4 hours in an inert gas atmosphere in a batch orcontinuous reactor to produce calcined coke; or (d) stepwise calcinationin a continuous calcining reactor between about 200° to about 1400° C.with up to about 1 hr residence time. Also disclosed are calcined cokesproduced by such methods.

This summary is provided to introduce a selection of concepts in asimplified form that are further described below in the detaileddescription. This summary is not intended to identify key features oressential features of the claimed subject matter, nor is it intended asan aid in determining the scope of the claimed subject matter.

BRIEF DESCRIPTION OF THE DRAWINGS

The patent or application file contains at least one drawing executed incolor. Copies of this patent or patent application publication withcolor drawing(s) will be provided by the Office upon request and paymentof the necessary fee.

FIG. 1 shows process diagram for making calcined coke from fastpyrolysis bio-oil as described below.

FIG. 2 shows FTIR spectra of distillate bottoms is, before and aftercalcination as described below.

FIG. 3 shows TPO plots of distillate bottoms, taken at various stages ofthe calcination process as described below.

FIG. 4 shows TPO plots of guayule distillate bottoms, taken for both thetwo-step and one-step calcination processes as described below.

FIG. 5(a) XRD spectra of distillate bottoms products, taken at differentstages of the calcination process, where FIG. 5(b) and FIG. 5(c) arezoomed in at the 43° and 78°, respectively, as described below.

FIG. 6(a, b, c, d) shows SEM images of calcined switchgrass distillatebottoms at various magnifications, indicative of sponge coke morphologyas described below, at 100× (FIG. 6a ), 2500× (FIGS. 6b ), and 5000×(FIG. 6c and FIG. 6d ), as described below.

FIG. 7(a) shows examples of biorenewable calcined coke cut and sandedfor multimeter measurements and FIG. 7(b) shows application of 6Vpotential across a piece of biorenewable calcined coke as describedbelow.

FIG. 8 shows measurement of a current-voltage (I-V) curve for a piece ofbiorenewable calcined coke as described below; Disk dimensions: d=30.3mm; t=4.3 mm.

DETAILED DESCRIPTION OF THE INVENTION

Disclosed are methods of producing calcined coke from bio-oil from abiomass feedstock, involving (1) subjecting the bio-oil to atmosphericdistillation (e.g., about 50° to about 400° C. (50° to 400° C.), about700 to about 800 torr (700 to 800 torr), preferably about 760 ton (760ton)) in a batch or continuous distillation unit (distillationapparatus) and/or subsequently to vacuum distillation (e.g., about 100°to about 400° C. (100° to 400° C.), about 20 to about 100 torr (20 to100 torr)) in a batch or continuous vacuum distillation unit to producecoke bottoms (vacuum distillation first and atmospheric distillationsecond is not practical), (2) subjecting said coke (i.e. distillationbottoms) to (a) devolatilization at about 400° to about 1000° C. (e.g.,400° to 1000° C., preferably about 900° to about 975° C. (900° to 975°C.), more preferably about 950° C. (950° C.)) for about 1 to about 30minutes (e.g., 1 to 30 minutes, preferably about 5 to about 15 minutes(5 to 15 minutes), more preferably about 6 minutes (6 minutes)) in aninert gas atmosphere (e.g., nitrogen, argon) in a reactor (e.g., furnaceor kiln) to produce devolatilized coke, optionally cooling thedevolatilized coke, removing the devolatilized coke from the reactor andoptionally crushing the devolatilized coke, and calcining saiddevolatilized coke at about 1100° C. to about 1400° C. (e.g., 1100° C.to 1400° C., preferably about 1200° C. to about 1250° C. (1200° C. to1250° C.), more preferably about 1200° C. (1200° C.)) for up to about 2hours (e.g., up to 2 hours) in an inert gas atmosphere in a reactor toproduce calcined coke; or (b) devolatilization at about 400° to about1000° C. (e.g., 400° to 1000° C., preferably about 900° to about 1000°C. (900° to 1000° C.), more preferably about 950° C. (950° C.)) forabout 1 to about 30 minutes (1 to 30 minutes, preferably about 5 toabout 10 minutes (5 to 10 minutes), more preferably about 6 minutes (6minutes)) in an inert gas atmosphere in a reactor to producedevolatilized coke and calcining the devolatilized coke at about 1100°C. to about 1400° C. (e.g., 1100° C. to 1400° C., preferably about 1200°C. to about 1250° C. (1200° C. to1250° C.), more preferably about 1200°C. (1200° C.)) for up to about 2 hours (up to 2 hours) in an inertatmosphere in the same reactor to produce calcined coke; or (c) heatingat about 250° to about 400° C. (e.g., 250° to 400° C., preferably about300° C. (300° C.)) for about 2 to about 10 hours (2 to 10 hours,preferably about 3 hours (3 hours)), then subsequent devolatilization atabout 400° to about 1000° C. (e.g., 400° to 1000° C., preferably atabout 550° C. (550° C.)) for about 0.5 to about 5 hr (0.5 to 5 hours,preferably about 1 hr (1 hr)) to produce devolatilized coke, thencalcining said devolatilized coke at about 1200° C. to about 1400° C.(e.g., 1200° C. to 1400° C., preferably at about 1200° C. (1200° C.))for up to about 2 hours (e.g., up to 2 hours, preferably about 1 hr (1hr)) in an inert gas atmosphere to produce calcined coke; or (d)calcination in a continuous calcining reactor between about 200° toabout 1400° C. (e.g., 200° to 1400° C., preferably about 500° to about1200° C. (500° to 1200° C.)) with up to about 1.5 hr (e.g., up to 1.5hr) residence time, preferably about 500° C. (e.g., 500° C.) for about30 minutes (e.g., 30 minutes), then about 800° C. (e.g., 800° C.) forabout 40 minutes (e.g., 40 minutes), then about 1200° C. (e.g., 1200°C.) for about 20 minutes (e.g., 20 minutes). Also disclosed are calcinedcokes produced by such methods.

A biomass feedstock is defined as any renewable, biological materialthat can be converted to another form of fuel or energy product. Biomassfeedstocks are the animal, plant, and algal materials used to derivefuels. Biomass is defined as living or recently dead organisms and anybyproducts of those organisms, plants, or animals. The term is generallyunderstood to exclude coal, oil, and other fossilized remnants oforganisms, as well as soils. In the context of biomass energy, the termgenerally refers to those crops, residues, and other biologicalmaterials (plant or animal) that can be used as a substitute for fossilfuels in the production of energy and other products. Biomass feedstocksinclude lignocellulosic materials and animal waste products orby-products. Biomass feedstocks include the plant and algal materialsused to derive fuels like ethanol, butanol, biodiesel, and otherhydrocarbon fuels. Examples of biomass feedstocks include corn starch,sugarcane juice, crop residues such as corn stover and sugarcanebagasse, purpose-grown grass crops, and woody plants. Lignocelluloserefers to plant dry matter (biomass), so called lignocellulosic biomass.It is composed of carbohydrate polymers (cellulose, hemicellulose), andan aromatic polymer (lignin). These carbohydrate polymers containdifferent sugar monomers (six and five carbon sugars) and they aretightly bound to lignin. Lignocellulosic biomass can be broadlyclassified into virgin biomass, waste biomass, and energy crops. Virginbiomass includes all naturally occurring terrestrial plants such astrees, bushes and grass. Waste biomass is produced as a low valuebyproduct of various industrial sectors such as agricultural (e.g., cornstover, sugarcane bagasse, straw, etc.), forestry (e.g., saw mill andpaper mill discards). Energy crops are crops with high yield oflignocellulosic biomass produced to serve as a raw material forproduction of second generation biofuel, examples include switch grass(Panicum virgatum) and Elephant grass. Animal by-products areagricultural by-products originating from livestock keeping. It includesamong others solid excreta of animals. Animal waste products includeanimal manure, animal manure solids, poultry litter, etc. Animal manurerefers to animal excrement (solid waste, dung) and urine, optionallywith animal bedding, spilled food, spilled water, and/or feathers. Thisincludes manure from, for example, chickens, turkeys, ducks, geese,swine, sheep, goats, cattle, dairy cows, horses, or rabbits. The animalmanure may be solid or liquid or a slurry. Animal manure solids refer tomanure solids that are present in a composition, such as poultry litteror an animal waste slurry, that contains manure. Solids content refersto the amount of solids present in a composition that remain after waterfrom the liquid is evaporated. There are cases where animal manuresolids exist that are not mixed with anything, such as in cattle feedlots. Poultry litter is a mixture of manure, bedding material (such assawdust, wood shavings, straw, recycled paper, nut hulls, or ricehulls), spilled food and feathers. Poultry litter is the bed of materialon which poultry, such as broiler chickens, are raised in commercialpoultry rearing facilities. Because the same bed of litter is often usedin successive growouts or flocks of poultry, the litter varies over timewith the addition of manure to the litter, the addition of bedding oramendments between growouts, and efforts to clean or de-cake the litterbetween growouts. “De-caking” refers to the process whereby a mechanicaldevice is used to sift the poultry litter between growouts to remove thelarger particles, which typically have a higher moisture content thanthe rest of the litter.

Pyrolysis to obtain bio-oil can be performed on a bubbling fluidized bedpyrolysis system, for example see the one previously described byBoateng et al. (Boateng, A. A., et al., Ind. Eng. Chem. Res., 46:1891-1897 (2007); Boateng, A. A., et al., Energy Fuels, 24: 6624-6632(2010); U.S. patent application Ser. No. 13/777,020, filed 26 Feb. 2013;Mullen, C. A., et al., Energy and Fuels, 27: 3867-3874 (2013)).Pyrolysis can be conducted at a fluidized bed temperature of betweenabout 450° and about 550° C. (e.g., 450° to 550° C.) andreaction/residence times from about 0.1 to about 5 seconds (e.g., 0.1 to5 seconds; preferably about 0.1 to about 1 second (e.g., 0.1 to 1second)). Control of the temperatures, and feed rate and data collectioncan be accomplished through use of standard control systems (e.g.,Siemens PCS7 control system). The pyrolysis reactor described above canbe modified for operation on recycled product gas by including aregenerative blower with an inlet port connected to the ESP outlet toreturn ESP tail gases to the fluidized bed plenum upon reheating throughan electric heater. A remotely controlled gas outlet valve in the blowerinlet line allows for the discharge of the preheated returned gases tomaintain a constant system volume. A pressure transmitter in the blowerinlet line can be integrated with the control system to modulate the gasoutlet valve. The regenerative blower can be sized to provide sufficientflow and head to fluidize the sand bed. The system can be flushed withan inert atmosphere (e.g., nitrogen) during heating to remove systemair. A small amount of nitrogen (<about 0.5 L/min) may be required toflow into the feed drop tube to maintain a positive pressure throughoutthe system as well as to aid feedstock flow. The amount ofnon-condensable gases recycled to the reactor may be about 10 to about99% (e.g., 10 to 99%), preferably about 40 to about 90% (e.g., 40 to90%), preferably about 60 to about 85% (e.g., 60 to 85%), preferablyabout 65 to about 80% (e.g., 65 to 80%), preferably about 70% (e.g.,70%) non-condensable gases to said reactor to produce deoxygenatedbio-oil.

“Optional” or “optionally” means that the subsequently described eventor circumstance may or may not occur, and that the description includesinstances in which said event or circumstance occurs and instances whereit does not. For example, the phrase “optionally comprising a defoamingagent” means that the composition may or may not contain a defoamingagent and that this description includes compositions that contain anddo not contain a foaming agent.

By the term “effective amount” of a compound or property as providedherein is meant such amount as is capable of performing the function ofthe compound or property for which an effective amount is expressed. Aswill be pointed out below, the exact amount required will vary fromprocess to process, depending on recognized variables such as thecompounds employed and the processing conditions observed. Thus, it isnot possible to specify an exact “effective amount.” However, anappropriate effective amount may be determined by one of ordinary skillin the art using only routine experimentation.

Unless defined otherwise, all technical and scientific terms used hereinhave the same meaning as commonly understood by one of ordinary skill inthe art to which the invention belongs. As used herein, the term “about”refers to a quantity, level, value or amount that varies by as much as30%, preferably by as much as 20%, and more preferably by as much as 10%to a reference quantity, level, value or amount. Although any methodsand materials similar or equivalent to those described herein can beused in the practice or testing of the present invention, the preferredmethods and materials are now described.

The following examples are intended only to further illustrate theinvention and are not intended to limit the scope of the invention asdefined by the claims.

EXAMPLES

Fast pyrolysis of biomass: Prior to fast-pyrolysis experiments, allfeedstocks were ground and dried. Switchgrass (SwG) feedstock wasprovided by the McDonnell Farm (East Greenville, Pa.), Eucalyptusbenthamii (Eucal) by Embrapa Forestry (Candoi, Parana, Brazil), andguayule bagasse (Guay) by Yulex (Chandler, Ariz.). Fast-pyrolysis offeedstock was carried out in the USDA fluidized bed fast pyrolysissystem, as described previously (Mullen, C. A., et al., Energy Fuels,27: 387-3874 (2013); U.S. patent application Ser. No. 13/777,020 filed26 Feb. 2013). Briefly, 2 kg/hr of feedstock is fed through a fluidizedsand bed reactor under 500° C., N₂ (FIG. 1a ). The resulting vapors thenpass through a cyclone which separates out char particulates. Liquidphases are then condensed from the vapor by four condensers in series.Oil precipitates from the non-condensable gases (NCGs) by twoelectrostatic precipitators (ESPs) in series. All experiments used theoil obtained from the ESPs. For tail-gas recycle experiments, a fractionof the non-condensable gas stream was mixed with the N₂ stream andrecycled into the fluidized bed, using a preheater and gas blower. Thepyrolysis system recycled the tail gas generally in the range of about50-70%. Unless specified otherwise, biomass samples underwent the TGRPprocess.

Bio-oil distillation: Bio-oil samples were distilled using either afractionating column or a short-path distilling head (Elkasabi, Y., etal., ACS Sustainable Chem. Eng., p. 10.1021/sc5002879 (2014)). Briefly,20, 50, or 100 g of bio-oil was heated in a round-bottom flask connectedto a distillation apparatus. Vapors were condensed and collected untilthe bottoms temperature reached 350° C. Then vacuum was applied, andmore vapors were condensed and collected. After removing the vacuum andturning off the heating mantle, the round-bottom flask was allowed tocool. The hard glassy bottoms residue was chipped, scraped, andcollected from the flask and crushed into a granular powder with amortar and pestle.

Devolatilization and calcination of distillate bottoms: Fordevolatilization, 1 to 5 g of each distillate bottoms sample was placedin a high-temperature crucible and then the crucible placed in a staticmuffle furnace. The oven with crucibles was purged of air with nitrogenbefore placing lids on crucibles. With continuous nitrogen flow, theoven temperature was gradually raised to 950° C. over a period ofapproximately 1 hr, then held at that temperature for 6 minutes beforethe crucibles were removed and cooled. Devolatilized products werecrushed into a powder for further analysis. For calcination, the sameprocedure was followed for either devolatilized bottoms or distillatebottoms, except that the temperature was gradually raised to atemperature of 1200° C. over a period of 3 hr (see FIG. 1). Thecrucibles were then held at 1200° C. for 1 hr, then the temperature wasvery gradually lowered to 400° C. before removing the crucibles from theoven in order to prevent crucible fracture. For one-step calcination,distillate bottoms underwent devolatilization and calcination in serieswithout any intermediate cooling step.

Characterization: Powder X-ray Diffraction (XRD) was performed onbottoms samples (as-is, devolatilized, calcined) using a Rigaku highsensitive D/teX Ultra with a scan rate of 6 degrees per minute.Elemental analysis (CHN) by combustion, as well as sulfur analysis bytitration, was carried out by Robertson Microlit Laboratories(Ledgewood, N.J.). Oxygen content was determined by difference. FTIRspectra of solid samples were obtained using a Nicolet Nexus 670 FTIRspectrometer (Madison, Wis.) with a Smart Orbit diamond attenuated totalreflection (ATR) accessory, DTGS KBr detector splitter, and KBrsplitter. Scanning electron microscopy images were taken using a Quanta200 FEG Environmental Scanning Electron Microscope. Higher heatingvalues of combustion were determined for distillate bottoms samplesusing a Leco AC600 bomb calorimeter. Ash content was determined byheating the sample in a crucible to 750-850° C. (ambient air) overnight.The mass remaining in the crucible was weighed, and this weight wasnormalized by the starting mass to calculate the % ash. Electricalconductivity measurements were performed using a CE Compass 305Dvariable DC power supply and a Cen-Tech P37772 multimeter. Calcinedsamples were cut into rectangles from a solid sample, and a colloidalsilver paint was applied to each end of the rectangular sample. Cutsamples were measured for electrical resistance across the length of thesample using a multimeter. Resistivity values were calculated based uponmeasurements of fixed, longitudinally-shaped samples.

Surface area measurements and temperature programmed oxidations wereperformed on a Quantachrome ASiQ with an attached Pfeiffer VacuumPrismaPlus mass spectrometer (Quantachrome Instruments, Boynton Beach,Fla.). Prior to surface area measurements, samples were outgassed for 12h at 200° C. Surface areas were then determined using the BET methodover the pressure range of 0.025<P/P₀<0.3. In a typical TPO analysis,about 12 mg of sample were placed in a sample tube sandwiched betweenpackings of quartz wool and dried and degassed at 120° C. under vacuumfor 20 min. Gas flow was then started using a mixture of 5% O₂ in helium(ILMO gas, Jacksonville, Ill.) set at a flow rate of 40 ml/min and thecell purged for 20 min prior to the start of the measurement. Under thisgas flow and at this starting temperature, the sample was heated at 10°C./min to 1050° C. The mass spectrometer outputs representing thefollowing m/e were recorded: 18 (H₂O), 28 (CO), 32 (O₂), and 44 (CO₂).X-ray fluorescence (XRF) was performed within a focused ion beam SEM(FEI Strata DB235) using an integrated x-ray fluorescence analyzer withseparate x-ray source for trace elemental analysis.

Results and Discussion. Coke Preparation Steps: Although all cokesamples originated from bio-oils of varying feedstock origins, we aimedto design a process for upgrading distillate bottoms such that allproducts converge towards similar compositions regardless of feedstockorigins. The main reason was to remove feedstock dependence from aneventual biorefinery, which would enhance technology transfer fromlocation to location. Calcined coke consists of >96% graphitized carbondomains, so all calcined bottoms products should theoretically beidentical. After performing atmospheric and vacuum distillations, asemi-liquid distillate with a jet black residue remained in the flask.Under vacuum, the residue resembled a molten viscous tar. When raised toatmospheric pressure and cooled quickly, the tar solidified into aglassy black solid. Chipping and grinding the solid was the onlypractical way of utilizing it for post-processing. For industrialpurposes, a continuous distillation process would handle the vacuumdistillate bottoms under raised temperature, in a manner very analogousto a traditional petroleum refinery.

Industrially, calcined coke is manufactured by feeding the cokeemanating from the petroleum residue or delayed coker (termed “greencoke”) into a rotary kiln. The kiln gradually heats the green coke underinert atmosphere through multiple temperature zones, each of whichserves a different purpose beginning from volatile evolution tostructural adjustments through grain growth. For our laboratory batchexperiments, we divided the heat treatment steps into multiple stages inorder to segregate the phases of coke transformation. As seen in FIG. 1,the first step consisted of removing any volatiles, such that only fixedcarbon remained behind. Since fixed carbon consists of very highmolecular weight polyaromatic hydrocarbons (PAHs), the devolatilizationstep serves the dual purpose of increasing the carbon percentage as wellas removal of volatile compounds from fixed carbon. A second step(calcination) was applied to the devolatilized bottoms, which served thepurposes of (1) eliminating any heteroatoms, (2) rearranging free carbonchains into polyaromatic domains resembling graphite, and (3) increasingthe size of the polyaromatic carbon domains. We also investigated aone-step calcination process, wherein the calcination occurs immediatelyafter the devolatilization without removing the devolatilized samplefrom the furnace. The devolatilization expands the fixed carbon andstretches it out to thinner strands for calcination, so we anticipatedthat the one-step calcination will have a fundamentally different effecton the coke quality and/or structure. This one-step investigation wasnecessary since it mimics temperature grading through a rotary kiln.

Elemental Analysis: Table 1 presents the elemental and proximateanalysis of the distillate bottoms at different processing stages.Comparisons can be made with typical values for petroleum coke (Table2). Distillate bottoms exhibited evidence of feedstock effects sincethey contain remnants of biomacromolecules; for example, guayulecontained higher concentrations of nitrogen. Overall, the bottomsproducts surprisingly exhibited properties which made them useful as-is.Via bomb calorimetry, the bottoms surprisingly possessed heating valuesbetween 32.6 and 36.4 MJ/kg, a significantly higher range than that oftraditional petroleum coke or coal (29.8 and 25.2 MJ/kg, respectively)(Andrews. A., and R. K. Lattanzio, “Petroleum Coke: Industry andEnvironmental Issues,” Congressional Research Service, 2013). Combinedwith the tail-gas from the TGRP process (HHV=12.4 MJ/kg) (Mullen, C. A.,et al., Energy Fuels, 27: 387-3874 (2013)), distillate bottoms can stillserve as fuel for the endothermic pyrolysis reaction to reduce heatdemand for a pyrolysis biorefinery.

The surprisingly low ash content and absence of sulfur enable distillatebottoms to be used for both fuel and higher quality cokes if the bottomscalcination step is optimized with respect to material properties.Devolatilization of the distillate bottoms produced a lustrous blacksolid which is usually indicative of greater structural order. Lossesdue to volatiles comprised at least 38% to upwards of 60% of thedistillate bottoms. While these percentages are considered relativelyhigh for asphalting applications, a partial devolatilization step isconceivable, which would remove a portion of the volatiles withoutfurther heating. Devolatilization surprisingly removed nearly all of theresidual hydrogen, oxygen was reduced to less than half the originalcontent, and nitrogen remained unchanged. It was only duringhigh-temperature calcination that the nitrogen content surprisingly fellsignificantly. Most importantly, the carbon percentages surprisinglyincreased for both devolatilization and calcination steps. The renewablecalcined coke resulting from this process surprisingly had propertiessimilar to calcined petroleum coke, but in addition had two propertieswhich surprisingly render it superior. Sulfur was surprisingly presentin only trace quantities (below 500 ppm), and for specific feedstocksthe ash/metals content surprisingly amounted to less than 0.7%, with lowconcentrations of specifically problematic metals such as vanadium,nickel, sodium, potassium, and calcium. Very low sulfur levels stronglybenefit aluminum smelting anodes, graphite, and steel metallurgy. Inaluminum smelting, sulfur reduces the reactivity of carbon anodes andproduces toxic SO₂ and COS gases. To make steel, coke used during therecarburizing step should be as low in sulfur as possible since itspresence causes brittleness in the final product. For graphitization ofcalcined coke, both sulfur and nitrogen induce “puffing” which ruins thestructural ordering (Ellis, P. J., and C. A. Paul, “Tutorial: PetroleumCoke Calcining and Uses of Calcined Petroleum Coke,” IN AIChE 2000Spring National Meeting,Third International Conference on RefiningProcesses, Session T9005, Atlanta, Ga., 2000). Although the nitrogen andoxygen levels could still be reduced further, these calcined bottomsproducts surprisingly resulted from only 1 hr of calcination at 1200°C., whereas smaller levels of heteroatoms (e.g., nitrogen, hydrogen,oxygen) can come about from higher temperatures and longer reactiontimes. Nevertheless, the results also surprisingly illustrated thegreater efficiency in process time and temperature for calciningdistillate bottoms as compared to petroleum coke. Elemental analysis(EA) results from the one-step procedure surprisingly produced similarresults, with no indication of improved carbon percentages. Yields ofdevolatilized bottoms ranged from 50 to 65%, depending on the startingvolatiles content. Calcination of devolatilized bottoms consistentlyresulted in an 85-87% yield across all bottoms samples, whichsurprisingly indicated the uniformity of the process into a definedproduct. Furthermore, HHV values for calcined products surprisingly allmeasured to be nearly identical values (around 33.3 MJ/kg) which, asnoted above, was significantly higher range than that of coal. Since HHVis directly related to atomic composition, the identical HHV valuessurprisingly demonstrated the convergence of all bottoms samples towardsa standardized end product (see also Table 8 below).

Metallic impurities can alter the application and/or final end-useproperties for calcined coke. For aluminum smelting anodes, theelectrolysis introduces the metal impurities into the aluminum productand affects the reduction efficiency (Hardin, E. E., and R. E. Gehlbach,“Calcined petroleum coke for the aluminum industry,” Great Lakes CarbonCorporation-Information Booklet, 1992); therefore aluminum smeltersrequire low ash and/or metals content. We employed x-ray fluorescence toelucidate the amount and types of metal impurities that make up the ash.Rather than directly scanning the coke samples, increased resolution andaccuracy were obtained by scanning the ash and using the results torecalculate concentrations for the coke samples. Table 3 displays theXRF trace metal analysis for detected metals in comparison with generalvalues for petroleum coke. In general, most metal concentrationssurprisingly fell close to or within limits typically found forpetroleum coke. Since steel is an alloy of iron, excess iron levels incalcined coke should only benefit the end composite. Greater incidencesof problematic concentrations of metallic impurities became morefrequent as the calcined ash content increased; specifically, calcinedcoke from pyrolysis liquids made from Eucalyptus benthamii containedrelatively low concentrations of only a few metals, whereas calcinedcoke from guayule bagasse had high concentrations of Si, K, Fe, and Cu.Vanadium and nickel are two specific metals which are heavily undesiredin the petrochemical and anode industries, due to catalyst poisoning andair reactivity, respectively (Mandal, P. C., et al., J. Japan Petrol.Inst., 1: 18-28 (2014)). Their levels in calcined bottoms surprisinglyremained mostly absent or at very low concentrations.

FTIR Spectroscopy: Due to the very heavy and conductive nature of thecalcined coke molecules, techniques for characterization were limited.Calcined coke (in general, and our product) is insoluble in every commonsolvent. We used FTIR to assess the presence of functional groups andchemical bonds in fresh distillate bottoms, as well as the predominantchemical bonds present in the structured calcined bottoms. Whilecalcined and/or graphitized cokes have been characterized by thecomplementary Raman spectroscopy method, recent studies have revealeduseful information with FTIR as well (Zhao, J., et al., Carbon, 47:744-751 (2009); Garcia, A. B., et al., Carbon, 47: 2563-2570 (2009);Sarkar, A., et al., Fuel, 117: 598-607 (2014)). FIG. 2 shows FTIRspectra for switchgrass distillate bottoms (as-is, calcined) andeucalyptus distillate bottoms (calcined). From the switchgrassdistillate bottoms spectrum, oxygenated species existed as alcoholgroups (3336 cm⁻¹), carbonyls (1684 cm⁻¹), and C—O linkages (1300-1000cm⁻¹); other functional groups included the C—H stretch (2962 cm⁻¹) andaromatic C—C (1595 and 1438 cm⁻¹). In contrast, the calcined samplesstudied always showed only two peaks: a singular aromatic C—C peak (1568cm⁻¹) and a C—O stretch (1092-1200 cm⁻¹). Although all samples containedaromatic C—C bonds, the number of C—C peaks were surprisingly reduced toa single broad band in calcined samples, which reflected two phenomena:(1) homogenization of chemical composition and structure, and (2)increased restriction of bond vibrations due to structural order. Whilethe oxygen content was relatively small in calcined samples, the C—Opeak at 1092 and/or 1200 usually appeared with strong intensity,compared with peaks of other functional groups. Hence, the C—C and C—Opeaks appeared to be of similar peak intensity. In addition, the twoFTIR bands corresponded well with the Raman shift values reported inliterature for calcined petroleum cokes (Zhao, J., et al., Carbon, 47:744-751 (2009)).

Temperature Programmed Oxidation (TPO): Temperature programmed oxidationis a method for observing oxidation trends and products as they relateto the structural and compositional properties. Oxidation temperaturesof carbonaceous solids are directly proportional to their degree ofstructural order (Garcia, A. B., et al., Carbon, 47: 2563-2570 (2009);Oliveira, H. A., et al., J. Braz. Chem. Soc., 23: 868-879 (2012); Chen,K., et al., Fuel, 113: 274-279 (2013)). We used TPO to evaluateoxidation resistance of coke samples by observing the oxidation productsproduced. Each sample was reacted under 5% oxygen in helium in order toobserve evolution of water and carbon oxides. FIG. 3 displays the TPOprofiles for bottoms from two different bio-oils throughout thecalcination process. For all bottoms samples, TPO profiles revealed agradual reduction in the amount of water produced until the calcinedsamples surprisingly produced no water, indicative of the high purity ofcarbon in calcined coke. Temperatures for peak oxygen consumption andignition temperature (i.e., onset of oxygen consumption) increased forboth devolatilization and calcination steps, indicating the role eachstep contributed towards structural improvement of distillate bottoms.While peak temperatures may exhibit slight variations due to differencesin sample size, the ignition temperature was not affected, and theignition temperatures confirmed the trends found with the peak oxygenconsumption temperatures.

Generally speaking, combustion of carbon into CO indicates a degree ofresistance against the complete oxidation into CO₂ (and hence so doesthe CO/CO₂ ratio). As-is, the distillate bottoms surprisingly exhibitedsignificantly greater levels of CO production relative to CO₂ ascompared with typical fast-pyrolysis biochar (Jackson, M. A., et al.,BioResources, 8: 5461-5474 (2013)). Since biochar (the side product fromfast pyrolysis) is heavily loaded with metals compared with distillatebottoms, biochar carbon morphology is amorphous, as indicated by its lowtemperature of oxidation (Chen, K., et al., Fuel, 113: 274-279 (2013)).The volatiles content of distillate bottoms played a role in theirhigher heating values by facilitating the combustion of the highermolecular weight carbon. This was evidenced by the significant increasein TPO combustion temperature in going from “as-is” to devolatilizedbottoms. Although the decrease in elemental oxygen content was muchgreater for the devolatilization step, the drop in CO/CO₂ ratio was muchgreater for the calcination step. This disparity indicated that the dropin CO/CO₂ ratio was likely due to the structural reordering rather thandue to a loss in reactive oxygen. Another clear indication of thestructural homogenization of calcined coke was the similarity of the COand CO₂ curves. In the bottoms, the CO and CO₂ profiles appeared toevolve independently whereas the two gases evolved in parallel in thedevolatilized and calcined samples.

With regards to one-step calcination, FIG. 4 displays the TPO of guayuledistillate bottoms through the calcination process in comparison with atwo-step calcination. While it appeared that the devolatilization stepsignificantly improved the structural ordering via the higher peaktemperature, the subsequent calcination step reduced the peak combustiontemperature to 810° C. while simultaneously segregating the coke intothree specific domains. On the other hand, the one-step proceduresurprisingly improved the morphological uniformity by increasing thepeak temperature and reducing it to a single curve, with the exceptionof the small peak at 530° C.

Crystallinity: Since calcination aims to improve the morphology of fixedcarbon, it is expected that the calcination process would quantitativelyimprove the structural order. In this regard, XRD is another criticalmethod for assessing any crystalline structures and/or hierarchicalorder. We used XRD to examine distillate bottoms at each stage of thecalcination process. FIG. 5 displays XRD spectra fromswitchgrass-derived distillate bottoms taken at each step of thecalcination process. Graphitic domains arrange according to a hexagonalstructure, so this structure was taken as the basis for interpretation(Li, Z. Q., et al., Carbon, 45: 1686-1695 (2007)). The (002) peak at2θ=22-26° indicated interlayer scattering across sheets within agraphite crystallite, whereas the (100) peak at 42-44° C. emanated fromintralayer scattering across the sheet (Adelhelm, P., Sci. Technol. Adv.Mater., 13: 1-8 (2012)). As the heat treatment of bottoms progressed,the (002) peak gradually decreased in full width at half maximum (FWHM)(FIG. 5a ), indicating a gradual increase in crystallite size.Similarly, the (100) peak appeared after devolatilization, then becamemore defined into two separate peaks upon calcination (43 and 52° FIG.5b ). A similar trend was seen for the peak at 78° (FIG. 5c ). Tocalculate the crystallite grain sizes L_(c), and L_(a), we can use theequations (2) developed by Short and Warlker for turbostratic carbons,where 2θ at (002) and (100) are used for L_(c) and L_(a), respectively:

$\begin{matrix}{L_{c} = {{\frac{0.45\;\lambda}{\Delta\;\sin\;\theta_{(002)}}\mspace{14mu} L_{a}} = \frac{0.92\;\lambda}{\Delta\;\sin\;\theta_{(100)}}}} & (2)\end{matrix}$Table 4 shows the calculated values for all samples. Thedevolatilization step increased the crystallite size, which simplyresulted from the absence of scattering from amorphous volatilies.However, more significant increases in crystallite size occurred forcalcination of devolatilized samples, indicating that the calcinationprocess effectively increased the structural order present within thesample. Most of the calcined samples approached >26 angstroms crystalgrain size, which correlates with required anode specifications forcalcined petroleum coke (Edwards, L., et al., “Evolution of anode gradecoke quality,” IN Light Metals 2012, Wiley, 2012, pp. 1207-1212). Inparticular, switchgrass-based samples showed the greatest increases ofcrystallite dimensions. One interesting correlation existed between theTPO and XRD results, in that an increase or decrease in the peak oxygenconsumption temperature resulted in a similar change for crystallitesizes. For example, guayule bagasse distillate bottoms crystallitesexhibited the greatest sizes when devolatilized, whereas the calcinedversion exhibited smaller sizes overall. Similarly, the TPO temperatureof combustion for devolatilized guayule bottoms greatly increased totemperatures near 1000° C., whereas the two-step calcined version onlyreached 810-875° C. One-step calcination of guayule bottoms producedboth a higher temperature stability and a larger crystallite size, thusfalling in line with the aforementioned trend. It is crucial to notethat the conditions used in these experiments (1200° C., 1 hr)represented relatively mild conditions for coke calcination, yetsurprisingly produced properties comparable to or better than calcinedpetroleum coke. Even better crystallite properties are expected to arisefrom longer calcination times and/or greater temperatures (e.g., about1200° to about 1400° C. (1200° to 1400° C.), about 1 to about 4 hr (1 to4 hr)) because the crystallite dimensions each follow tightly lineartrends with respect to processing temperature (Feret, F. R., Analyst,123: 595-600 (1998); Ellis, P. J., and C. A. Paul, “Tutorial: PetroleumCoke Calcining and Uses of Calcined Petroleum Coke,” IN AIChE 2000Spring National Meeting,Third International Conference on RefiningProcesses, Session T9005, Atlanta, Ga., 2000). Another more accuratemethod for calculating the crystallite size is based on the methods usedfor calcined petroleum coke, rather than the method for nanostructuredcarbon as mentioned earlier. When employing equation (3) from the ASTMstandard of calculating L_(c), the crystallite

$\begin{matrix}{L_{c} = {{\frac{0.89\;\lambda}{\Delta\;\cos\;\theta_{(002)}}\mspace{14mu} L_{a}} = \frac{1.84\;\lambda}{\Delta\;\cos\;\theta_{(100)}}}} & (3)\end{matrix}$dimensions are directly comparable to any analysis of industrialcalcined coke. While the final crystallite sizes (Table 5) were slightlyless than the target values of 24 A, the results illustrated thepositive effect of calcination on crystalline structure, by way of thegradual increases in L_(c).

Morphology by SEM: Variations in coke morphology play critical roles intheir end-use properties. Sponge coke, a coke that is highly porous witha sponge-like appearance, is predominantly preferred in the petcokeindustry. Aluminum smelting anodes rely on the sponge coke porosity fordiffusion and adhesion of additives like pitch and binders into the cokebefore the anode is fully baked into a finished product (Ellis, P. J.,and C. A. Paul, “Tutorial: Petroleum Coke Calcining and Uses of CalcinedPetroleum Coke,” IN AIChE 2000 Spring National Meeting,ThirdInternational Conference on Refining Processes, Session T9005, Atlanta,Ga., 2000). In contrast, shot coke consists of hard pellets (2-4 mm),which is undesired for many applications. We assessed the morphology ofcoke samples via images taken by SEM (FIG. 6). The largest magnificationimage showed that the fragments were irregularly shaped and sized tomuch less than the 1 mm scale bar, in contrast to the large pelletsfound in shot coke. Higher magnification images revealed predominantsections of coke with bubble-like appearances, in addition to a porousstructure reflective of sponge coke morphologies. There was uniquenessin the SEM data since nearly all of the calcined coke was “sponge coke”morphology, and the prior art has all products being a mixture of spongecoke and shot coke morphologies. While BET surface area measured to berelatively low for devolatilized samples (10-20 m²/g), wider variationsoccurred for some calcined samples (150-300 m2/g). Low porosities aredesired, so optimization of both the temperature heat-up rate andpost-calcination grinding steps may be necessary (Ellis, P. J., and C.A. Paul, “Tutorial: Petroleum Coke Calcining and Uses of CalcinedPetroleum Coke,” IN AIChE 2000 Spring National Meeting,ThirdInternational Conference on Refining Processes, Session T9005, Atlanta,Ga., 2000); Cannova, F., et al., “Calcined coke particle size andcrushing steps affect its vbd result,” IN Light Metals 2011, Wiley,2011, pp. 937-939).

Electrical conductivity: Ultimately, an assessment of end-useapplications for calcined distillate bottoms requires measurement ofend-use properties. To this end, electrical conductivity measurementswere performed on switchgrass samples calcined in one-step. Thesesamples effectively kept the calcined coke constricted to a solid porousphase that was amenable to cutting and shaping. Long rectangular sampleswere cut out in order to ensure accurate resistivity calculations, and acolloidal silver paint on opposing faces ensured even distribution ofcurrent flow across the sample width. When applied to samples of variousdimensions and aspect ratios, an apparent resistivity value of 1.5 mΩ-m(+/−0.34) was obtained, which surprisingly meets the requirements forcalcined coke properties. If we further consider that the calcinedmaterial comprises of a porous network with air (an insulator) fillingthe voids, the resistivity reduces even further, in proportion to theporosity.

FIG. 7(a) shows representative cut samples of biorenewable calcined cokeused for resistivity measurements. The ends where resistancemeasurements were taken were first coated with silver paint to allow foruniform current distribution upon current entry and exit. Table 6 showsthe measured dimensions of cut calcined coke samples as well as theircorresponding resistivity values. The resistivity ρ is calculated fromequation (S1):

$\begin{matrix}{\rho = {R\frac{wh}{\iota}}} & ({S1})\end{matrix}$FIG. 7(b) is a visual example of how efficiently the calcined productconducted electricity. When connecting two metal wires to the terminalsof a 6V battery, simply touching the ends of these wires to the calcinedproduct produced a glow due to current flow. To quantify the performanceas an electrical conductor, a uniform solid disk of biorenewablecalcined coke was connected to a variable DC current source andmultimeter probes were simultaneously connected to the DC connectionclamps. As the current was incrementally increased, the voltageincreased in a linear fashion (FIG. 7). After the DC current reached 2.5amperes, the trend deviated from linear due to increasing temperaturesfrom resistive heating. Since this example did not use a clear geometryfor current entry and exit, resistivity values cannot be easilycalculated from the I-V curve.

It is important to note that for the starting bottoms material and forthe bottoms samples that were only devolatilized, none of theaforementioned electrical behaviors were observed. Hence, thecalcination process was critical for influencing the final productproperties.

Measurement of metals via x-ray fluorescence (XRF) of the ash provided adirect method for high-resolution measurement, provided that theoriginal concentrations are back-calculated correctly. Sulfur cannot bemeasured in this method since ashing oxidizes the sulfur into a gaseousproduct. Table 7 shows XRD direct measurements on the calcined cokeitself alongside the results from ash XRF. These values confirm and/orare similar to each other. With the exception of copper, both the directand ash measurements fall within 500 ppm of each other. Furthermore,sulfur was surprisingly measured to be 306 ppm, which also confirmed thesulfur concentration that is below the 500 ppm threshold for theprevious method of sulfur detection.

Experimental for Table 8: followed a one-step calcination procedure,wherein the distillate bottoms were heated in an inert N2 environment atabout 480° C. for 20 min, then heated to 1200° C. for 2.5 hr, thengradually cooled back to 600° C. before removal. Table 8 shows elementaland ash testing results for yet a fourth feedstock: horse litter TGRPbio-oil. When calcined for a longer time (2.5 hr), the carbon purityattained was surprisingly the highest from all other previouslymentioned results (98.6% C). Similarly, the % oxygen at 0.4% wassurprisingly the lowest attained.

Conclusions: We have demonstrated the synthesis and end-use propertiesof calcined coke obtained from bio-oil distillate bottoms. From thevarious bio-oils that were distilled, we surprisingly converted thebottoms from various bio-oils into products nearly identical incomposition and structure. These calcined cokes were surprisinglysuperior to calcined petroleum coke by virtue of their low sulfur (traceamounts) and metals content (0.2-1.1 wt %). Characterization by FTIRindicated an initial presence of oxygenated functional groups thatdisappeared upon calcination, leaving only a dominant aromatic carbonpeak with a minor C—O peak. TPO studies confirmed the progressivestabilization and structural ordering that the calcination processintroduced into the distillate bottoms. A one-step calcination processwas preferred, wherein the devolatilized samples were immediatelycalcined in situ. Significant crystallite growth occurred for bothdevolatilization and calcination steps, verified by XRD. SEM imagesrevealed a highly porous structure within sub-mm particles that rendersthat coke useful for mixtures with carbon anode binders. The electricalconductivity of biorenewable coke enables its application as a valuablesubstitute for calcined petroleum coke. The lack of any need fordesulfurization makes this a valuable process for many industries thatuse calcined petroleum coke.

Thus in this study, we demonstrated a straightforward conversion ofbio-oil distillate bottoms into calcined coke. The higher heating valuesof distillate bottoms produced “as-is” significantly exceeded that ofcoal or petroleum coke (HHV=36 MJ/kg, vs. 27 MJ/kg). To evaluate itsuses other than fuel, the solid residue was subjected to calcination at1200° C. for 1 hour under N₂ atmosphere. The resulting solid productnamed “biocoke” was composed of 96-99% carbon, was free from sulfur(<500 ppm), and contained 0.2-1.1% ash. X-ray diffraction of the biocokeconfirmed a steady increase in grain size with both devolatilization andwith calcination. FTIR spectroscopy indicated a total loss of functionalgroups with the calcination step, except two broad peaks representingC—C and C—O. Temperature programmed oxidation (TPO) of the bottomsbefore and after calcination illustrated an increasing structural ordervia the increasing temperature(s) necessary to oxidize the samples.Images from SEM revealed a bubbly morphology similar to theindustrially-favored sponge coke. The electrical resistivity of calcinedcoke samples measured to be <1.5 mΩ-m, which falls in line withspecifications for carbon anodes. Biorenewable calcined coke is animproved alternative to petroleum coke and can find application incarbon anodes, steel carburization, and graphite synthesis.

All of the references cited herein, including U.S. Patents, areincorporated by reference in their entirety.

Thus, in view of the above, there is described (in part) the following:

A method of producing calcined coke from bio-oil from a biomassfeedstock, said method comprising (or consisting essentially of orconsisting of) (1) subjecting said bio-oil to atmospheric distillationin a batch or continuous distillation unit and/or subsequently to vacuumdistillation in a batch or continuous vacuum distillation unit toproduce coke bottoms, (2) subjecting said coke bottoms to (a)devolatilization at about 400° to about 1000° C. for about 1 to about 30minutes in an inert gas atmosphere in a reactor to produce devolatilizedcoke, optionally cooling said devolatilized coke, removing saiddevolatilized coke from said reactor and optionally crushing saiddevolatilized coke, and calcining said devolatilized coke at about 1200°C. to about 1400° C. for up to 2 hours in an inert gas atmosphere in areactor to produce calcined coke; or (b) devolatilization at about 400°to about 1000° C. for about 1 to about 30 minutes in an inert gasatmosphere in a reactor to produce devolatilized coke and calcining saiddevolatilized coke at about 1200° C. to about 1400° C. for up to 2 hoursin an inert gas atmosphere in the same reactor to produce calcined coke;or (c) heating at about 250 to about 400° C. for about 2 to about 10hours, then subsequent devolatilization at about 400 to about 1000° C.for about 0.5 to about 5 hr to produce devolatilized coke, thencalcining said devolatilized coke at about 1200° C. to about 1400° C.for up to about 2 hours in an inert gas atmosphere to produce calcinedcoke; or (d) stepwise calcination in a continuous calcining reactorbetween about 200 to about 1400° C. with up to about 1 hr residencetime. The above method, comprising (a) devolatilization at about 400° toabout 1000° C. for about 1 to about 30 minutes in an inert gasatmosphere in a reactor to produce devolatilized coke, optionallycooling said devolatilized coke, removing said devolatilized coke fromsaid reactor and optionally crushing said devolatilized coke, andcalcining said devolatilized coke at about 1200° C. to about 1400° C.for up to 2 hours in an inert gas atmosphere in a reactor to producecalcined coke. The above method, comprising (b) devolatilization atabout 400° to about 1000° C. for about 1 to about 30 minutes in an inertgas atmosphere in a reactor to produce devolatilized coke and calciningsaid devolatilized coke at about 1200° C. to about 1400° C. for up to 2hours in an inert gas atmosphere in the same reactor to produce calcinedcoke. The above method, comprising (c) heating at about 250 to about400° C. for about 2 to about 10 hours, then subsequent devolatilizationat about 400 to about 1000° C. for about 0.5 to about 5 hr to producedevolatilized coke, then calcining said devolatilized coke at about1200° C. to about 1400° C. for up to about 2 hours in an inert gasatmosphere to produce calcined coke. The above method, comprising (d)stepwise calcination in a continuous calcining reactor between about 200to about 1400° C. with up to about 1 hr residence time.

The above method, where said calcined coke contains about 96 to about100% carbon (e.g., 96-100%). The above method, where said calcined cokecontains at least about 96% carbon (e.g., at least 96%). The abovemethod, where said calcined coke contains at least about 97% carbon(e.g., at least 97%). The above method, where said calcined cokecontains at least about 98% carbon (e.g., at least 98%). The abovemethod, where said calcined coke contains about 0 to about 1.5 wt %nitrogen (e.g., 0 to 1.5 wt %). The above method, where said calcinedcoke contains less than about 1.5 wt % nitrogen (e.g., less than 1.5wt%). The above method, where said calcined coke contains about 1 wt %nitrogen (e.g., 1 wt %). The above method, where said calcined cokecontains about 0.5 wt % nitrogen (e.g., 0.5 wt %). The above method,where said calcined coke contains about 0 to about 3 wt % oxygen (e.g.,0 to 3 wt %). The above method, where said calcined coke contains lessthan about 2 wt % oxygen (e.g., less than 2 wt %). The above method,where said calcined coke contains less than about 1.5 wt % oxygen (e.g.,less than 1.5 wt %). The above method, where said calcined coke containsless than about 1 wt % oxygen (e.g., less than 1 wt %). The abovemethod, where said calcined coke contains about 0.5 wt % oxygen (e.g.,0.5 wt %). The above method, where said calcined coke contains about 0to about 2000 ppm iron (e.g., 0 to 2000 ppm). The above method, wheresaid calcined coke contains less than about 1700 ppp iron (e.g., lessthan 1700 ppm). The above method, where said calcined coke contains lessthan about 1500 ppp iron (e.g., less than 1500 ppm). The above method,where said calcined coke contains about 200 to about 500 ppm sulfur(e.g., 200 to 500 ppm). The above method, where said calcined cokecontains less than about 500 ppm sulfur (e.g., less than 500 ppm). Theabove method, where said calcined coke contains less than about 300 ppmsulfur (e.g., less than 300 ppm). The above method, where said calcinedcoke contains about 0 to about 200 ppm vanadium (e.g., 0 to 200 ppm).The above method, where said calcined coke contains less than about 150ppm vanadium (e.g., less than 150 ppm). The above method, where saidcalcined coke contains about 0 to about 300 ppm nickel (e.g., 0 to 300ppm). The above method, where said calcined coke contains less thanabout 280 ppm nickel (e.g., less than 280ppm). The above method, wheresaid calcined coke contains about 0 to about 100 ppm sodium (e.g., 0 to100 ppm). The above method, where said calcined coke contains less thanabout 10 ppm sodium (e.g., less than 10 ppm). The above method, wheresaid calcined coke contains about 100 to about 500 ppm calcium (e.g.,100 to 500 ppm). The above method, where said calcined coke containsless than about 400 ppm calcium (e.g., less than 400 ppm). The abovemethod, where said calcined coke contains less than about 250 ppmcalcium (e.g., less than 250 ppm). The above method, where said calcinedcoke contains about 0.02 to about 1.1% ash (e.g., 0.02 to 1.1%). Theabove method, where said calcined coke contains less than about 1.1% ash(e.g., less than 1.1%). The above method, where said calcined cokecontains less than about 1% ash (e.g., less than 1%). The above method,where said calcined coke contains less than about 0.5% ash (e.g., lessthan 0.5%). The above method, where said calcined coke contains lessthan about 0.4% ash (e.g., less than 0.4%). The above method, where saidcalcined coke contains less than about 0.2% ash (e.g., less than 0.2%).The above method, where said calcined coke has less than about 2Ω-mmelectrical resistivity (e.g., less than 2Ω-mm). The above method, wheresaid calcined coke has about 1 to about 2Ω-mm electrical resistivity(e.g., 1 to 2Ω-mm). The above method, where said calcined coke has HHVof about 30 to 40 MJ/kg). The above method, wherein said calcined cokehas HHV of about 36 MJ/kg (e.g., 36 MJ/kg). The above method, where saidcalcined coke has HHV of about 33.3 MJ/kg (e.g., 33.3 MJ/kg). The abovemethod, where said calcined coke contains about 0 to about 4 wt %hydrogen (e.g., 0 to 4 wt %). The above method, where said calcined cokecontains less than about 4 wt % hydrogen (e.g., less than 4 wt %). Theabove method, where said calcined coke contains less than about 1 wt %hydrogen (e.g., less than 1 wt %). The above method, where said biomassfeedstock is selected from the group consisting of lignocellulosicbiomass, animal waste products, and mixtures thereof.

The above amounts and ranges are not meant to be limiting, andincrements between the recited percentages and ranges are specificallyenvisioned as part of the invention.

The above method, where said bio-oil is produced by a method comprising(or consisting essentially of or consisting of) (1) pyrolyzing saidfeedstock in an inert atmosphere in a reactor to produce bio-oil,bio-char and non-condensable gases; (2) recycling about 10 to about 99%of said non-condensable gases to said reactor to produce deoxygenatedbio-oil; wherein said method is conducted in the absence of oxygen andwherein said method does not utilize externally added catalysts.

Calcined coked produced by the above method.

Other embodiments of the invention will be apparent to those skilled inthe art from a consideration of this specification or practice of theinvention disclosed herein. It is intended that the specification andexamples be considered as exemplary only, with the true scope and spiritof the invention being indicated by the following claims.

TABLE 1 Chemical and physical properties of petroleum-derived cokeproducts and pyrolysis-derived biochar. Petroleum coke Biochar (Raw)(Calcined) (SwG) C 90 >96 63.1 H <4 <0.1 3.7 N 2-3 1-1.5 0.78 O   1-1.50 5.6 S 3 3 — HHV (MJ/kg) 31.3 — 20.1 % ash <0.4 <0.4 26.9 % volatiles10-12 <0.4

TABLE 2 Characterization of distillate bottoms products at variousstages of the calcinations process. (SwG = switchgrass, Eucal =eucalyptus, Guay = guayule, all using TGRP process. SwG-reg =switchgrass using traditional pyrolysis) Bottoms Devolatilized CalcinedSwG Eucal Guay SwG-reg SwG Eucal Guay SwG Eucal Guay SwG-reg C 86.8284.32 80.09 71.09 93.77 95.07 93.08 96.06 97.78 97.26 93.06 H 4.9 5.47.19 4.3 0.72 0.32 0.82 0.89 0.53 0.31 0.18 N 1.31 0.41 2.9 1.05 1.320.77 2.83 0.57 0.34 1.04 0.52 O 6.97 9.87 9.82 23.56 4.19 3.84 3.27 2.481.35 1.39 6.24 S <0.05 <0.05 <0.05 HHV (MJ/kg) 36.4 34.4 32.6 29.0 32.934.5 34.0 33.3 33.4 33.4 33.3 % ash 0.7 0.2 1.1 0.3

TABLE 3 Metals content of calcined distillate bottoms samples, asdetermined by XRF of ash. Values are compared with generalspecifications for petroleum coke. metal (ppm) SwG Eucal Guay petcoke*Na — — — <100 Si 884 tr 510 <250 K 296 321 1298 Ca 250 113 414 <200 V —— 148 <300 Cr — — 133 Fe 1424 395 1678 <300 Ni 220 — 277 <200 Cu 432 2271460 Zn 917 — 569 *Note that different companies give differentspecifications for their prior art.

TABLE 4 Crystal size parameters of distillate bottoms, calculated basedon XRD results. Bottoms Devolatilized Calcined length (A) SwG SwG-REucal Guay SwG SwG-R Eucal Guay SwG SwG-R Eucal Guay d 3.81 4.03 3.983.73 3.68 3.83 3.66 3.69 3.57 3.76 3.80 3.61 L_(c) 18.2 22.5 18.4 27.621.9 20.9 26.5 22.5 33.7 22.4 24.8 25.6 L_(a) 18.7 17.6 26.9 27.5 29.326.7 28.4 39.8 69.6 41.8 46.2 29.7

TABLE 5 Measured values of shaped calcined coke samples; the resistivityvalues (ρ) are calculated based upon the measured dimensions andelectrical resistances. L (mm) w h R (Ω) ρ (Ω-mm) 21.7 7.1 3.9 1.2 1.5320 7 4 1.1 1.54 15.2 3.8 2.6 2 1.30 10.4 5.5 3.6 1.1 2.09 Average 1.62St dev 0.34

TABLE 6 Comparison of XRF elemental concentrations in SwG calcined coke,as measured directly on the sample vs. measured from the sample ash.SwG-calcined SwG-calcined, f/sample f/ash Na 194 Mg Si 507 884 P S 306 K258 296 Ca 250 V Fe 941 1424 Ni 259 220 Cu 1012 432

TABLE 7 Proximate and total analysis of bottoms obtained from distillinghorse litter TGRP oil. This calcination was performed at 1200° C. for2.5 hr. Horse litter Horse litter bottoms bottoms, calcined C 79.0798.64 H 5.66 0.23 N 1.27 0.72 O 14.00 0.41 S <0.05 % ash 0.49

We claim:
 1. A method of producing calcined coke from bio-oil from abiomass feedstock, said method comprising (1) subjecting said bio-oil toatmospheric distillation in a batch or continuous distillation unitand/or subsequently to vacuum distillation in a batch or continuousvacuum distillation unit to produce coke bottoms, wherein the oxygen insaid bio-oil has not been removed from said bio-oil prior to saidatmospheric distillation and said vacuum distillation, (2) subjectingsaid coke bottoms to (a) devolatilization at about 400° to about 1000°C. for about 1 to about 30 minutes in an inert gas atmosphere in areactor to produce devolatilized coke, optionally cooling saiddevolatlized coke, removing said devolatilized coke from said reactorand optionally crushing said devolatilized coke, and calcining saiddevolatilized coke at about 1200° C. to about 1400° C. for up to about 2hours in an inert gas atmosphere in a reactor to produce calcined coke;or (b) devolatilization at about 400° to about 1000° C. for about 1 toabout 30 minutes in an inert gas atmosphere in a reactor to producedevolatilized coke and calcining said devolatilized coke at about 1200°C. to about 1400° C. for up to about 2 hours in an inert gas atmospherein the same reactor to produce calcined coke; or (c) heating at about250° to about 400° C. for about 2 to about 10 hours, then subsequentdevolatilization at about 400° to about 1000° C. for about 0.5 to about5 hr to produce devolatilized coke, then calcining said devolatilizedcoke at about 1200° C. to about 1400° C. for up to about 2hours in aninert gas atmosphere to produce calcined coke; or (d) calcination in acontinuous calcining reactor between about 200° about 1400° C. with upto about 1 hr residence time to produce calcined coke; where saidcalcined coke contains less than about 500 ppm sulfur.
 2. The methodaccording to claim 1, where said calcined coke contains about 96to about100% carbon.
 3. The method according to claim 1, where said calcinedcoke contains at least about 96% carbon.
 4. The method according toclaim 1, where said calcined coke contains at least about 97% carbon. 5.The method according to claim 1, where said calcined coke contains atleast about 98% carbon.
 6. The method according to claim 1, where saidcalcined coke contains about 0 to about 1.5 wt % nitrogen.
 7. The methodaccording to claim 1, where said calcined coke contains less than about1.5 wt % nitrogen.
 8. The method according to claim 1, where saidcalcined coke contains about 1 wt % nitrogen.
 9. The method according toclaim 1, where said calcined coke contains about 0.5 wt % nitrogen. 10.The method according to claim 1, where said calcined coke contains about0 to about 3 wt % oxygen.
 11. The method according to claim 1, wheresaid calcined coke contains less than about 2 wt % oxygen.
 12. Themethod according to claim 1, where said calcined coke contains less thanabout 1.5 wt % oxygen.
 13. The method according to claim 1, where saidcalcined coke contains less than about 1 wt % oxygen.
 14. The methodaccording to claim 1, where said calcined coke contains less than about0.5 wt % oxygen.
 15. The method according to claim 1, where saidcalcined coke contains about 0 to about 2000 ppm iron.
 16. The methodaccording to claim 1, where said calcined coke contains less than about1700 ppp iron.
 17. The method according to claim 1, where said calcinedcoke contains less than about 1500 ppp iron.
 18. The method according toclaim 1, where said calcined coke contains less than about 300 ppmsulfur.
 19. The method according to claim 1, where said calcined cokecontains about 0 to about 200 ppm vanadium.
 20. The method according toclaim 1, where said calcined coke contains less than about 150 ppmvanadium.
 21. The method according to claim 1, where said calcined cokecontains about 0 to about 300 ppm nickel.
 22. The method according toclaim 1, where said calcined coke contains less than about 280 ppmnickel.
 23. The method according to claim 1, where said calcined cokecontains about 0 to about 100 ppm sodium.
 24. The method according toclaim 1, where said calcined coke contains less than about 10 ppmsodium.
 25. The method according to claim 1, where said calcined cokecontains about 100 to about 500 ppm calcium.
 26. The method according toclaim 1, where said calcined coke contains less than about 400 ppmcalcium.
 27. The method according to claim 1, where said calcined cokecontains less than about 250 ppm calcium.
 28. The method according toclaim 1, where said calcined coke contains about 0.02 to about 1.1% ash.29. The method according to claim 1, where said calcined coke containsless than about 1.1% ash.
 30. The method according to claim 1, wheresaid calcined coke contains less than about 1% ash.
 31. The methodaccording to claim 1, where said calcined coke contains less than about0.5% ash.
 32. The method according to claim 1, where said calcined cokecontains less than about 0.4% ash.
 33. The method according to claim 1,where said calcined coke contains less than about 0.2% ash.
 34. Themethod according to claim 1, where said calcined coke has less thanabout 2 Ω-mm electrical resistivity.
 35. The method according to claim1, where said calcined coke has about 1 to about 2 Ω-mm electricalresistivity.
 36. The method according to claim 1, where said calcinedcoke has HHV of about 36 MJ/kg.
 37. The method according to claim 1,where said calcined coke has HHV of about 33.3 MJ/kg.
 38. The methodaccording to claim 1, where said calcined coke contains about 0 to about4 wt % hydrogen.
 39. The method according to claim 1, where saidcalcined coke contains less than about 4 wt % hydrogen.
 40. The methodaccording to claim 1, where said calcined coke contains less than about1 wt % hydrogen.
 41. The method according to claim 1, where said biomassfeedstock is selected from the group consisting of lignocellulosicbiomass, animal waste products, and mixtures thereof.
 42. The methodaccording to claim 1, where said bio-oil is produced by a methodcomprising (1) pyrolyzing said feedstock in an inert atmosphere in areactor to produce bio-oil, bio-char and non-condensable gases; (2)recycling about 10 to about 99% of said non-condensable gases to saidreactor to produce deoxygenated bio-oil; wherein said method isconducted in the absence of oxygen and wherein said method does notutilize externally added catalysts.
 43. Calcined coked produced by themethod according to claim 1, where said calcined coke contains less thanabout 500 ppm sulfur.
 44. The method according to claim 1, where saidmethod comprises (1) subjecting said bio-oil to atmospheric distillationin a batch or continuous distillation unit and/or subsequently to vacuumdistillation in a batch or continuous vacuum distillation unit toproduce coke bottoms, (2) subjecting said coke bottoms to (a)devolatilization at about 400° to about 1000° C. for about 1 to about 30minutes in an inert gas atmosphere in a reactor to produce devolatilizedcoke, optionally cooling said devolatlized coke, removing saiddevolatilized coke from said reactor and optionally crushing saiddevolatilized coke, and calcining said devolatilized coke at about 1200°C. to about 1400° C. for up to about 2 hours in an inert gas atmospherein a reactor to produce calcined coke.
 45. The method according to claim1, where said method comprises (1) subjecting said bio-oil toatmospheric distillation in a batch or continuous distillation unitand/or subsequently to vacuum distillation in a batch or continuousvacuum distillation unit to produce coke bottoms, (2) subjecting saidcoke bottoms to (b) devolatilization at about 400° to about 1000° C. forabout 1 to about 30 minutes in an inert gas atmosphere in a reactor toproduce devolatilized coke and calcining said devolatilized coke atabout 1200° C. to about 1400° C. for up to about 2 hours in an inert gasatmosphere in the same reactor to produce calcined coke.
 46. The methodaccording to claim 1, where said method comprises (1) subjecting saidbio-oil to atmospheric distillation in a batch or continuousdistillation unit and/or subsequently to vacuum distillation in a batchor continuous vacuum distillation unit to produce coke bottoms, (2)subjecting said coke bottoms to (c) heating at about 250° to about 400°C. for about 2 to about 10 hours, then subsequent devolatilization atabout 400° to about 1000° C. for about 0.5 to about 5 hr to producedevolatilized coke, then calcining said devolatilized coke at about1200° C. to about 1400° C. for up to about 2 hours in an inert gasatmosphere to produce calcined coke.
 47. The method according to claim1, where said method comprises (1) subjecting said bio-oil toatmospheric distillation in a batch or continuous distillation unitand/or subsequently to vacuum distillation in a batch or continuousvacuum distillation unit to produce coke bottoms, (2) subjecting saidcoke bottoms to (d) calcination in a continuous calcining reactorbetween about 200° about 1400° C. with up to about 1 hr residence timeto produce calcined coke.
 48. The method according to claim 1, wheresaid method comprises (1) subjecting said bio-oil to atmosphericdistillation in a batch or continuous distillation unit at about 50° toabout 400° C. and about 700 to about 800 torr and/or subsequently tovacuum distillation in a batch or continuous vacuum distillation unit atabout 100° to about 400° C. and about 20 to about 100 torr to producecoke bottoms.
 49. A method of producing calcined coke from bio-oil froma biomass feedstock, said method comprising (1) subjecting said bio-oilto atmospheric distillation in a batch or continuous distillation unitand/or subsequently to vacuum distillation in a batch or continuousvacuum distillation unit to produce coke bottoms, (2) subjecting saidcoke bottoms to (a) devolatilization at about 400° to about 1000° C. forabout 1 to about 30 minutes in an inert gas atmosphere in a reactor toproduce devolatilized coke, optionally cooling said devolatlized coke,removing said devolatilized coke from said reactor and optionallycrushing said devolatilized coke, and calcining said devolatilized cokeat about 1200° C. to about 1400° C. for up to about 2 hours in an inertgas atmosphere in a reactor to produce calcined coke; or (b)devolatilization at about 400° to about 1000° C. for about 1 to about 30minutes in an inert gas atmosphere in a reactor to produce devolatilizedcoke and calcining said devolatilized coke at about 1200° C. to about1400° C. for up to about 2 hours in an inert gas atmosphere in the samereactor to produce calcined coke; or (c) heating at about 250° to about400° C. for about 2 to about 10 hours, then subsequent devolatilizationat about 400° to about 1000° C. for about 0.5 to about 5 hr to producedevolatilized coke, then calcining said devolatilized coke at about1200° C. to about 1400° C. for up to about 2hours in an inert gasatmosphere to produce calcined coke; or (d) calcination in a continuouscalcining reactor between about 200° about 1400° C. with up to about 1hr residence time to produce calcined coke; where said calcined cokecontains less than about 500 ppm sulfur.
 50. The calcined cokedaccording to claim 43, where said calcined coke contains less than about300 ppm sulfur.